A method for producing decomposed liquid and / or gaseous hydrocarbons from feedstock including waste plastics and / or waste rubber, or a pyrolysis gasification / oil conversion apparatus for the same purpose.

Abstract

The present invention provides a method for producing decomposed liquid and / or gaseous hydrocarbons from supply materials including waste plastics and / or waste rubber, the method having high efficiency and / or high recyclability, and an apparatus for carrying out the said method. [Solution] A method for producing decomposed liquid and / or gaseous hydrocarbons from feedstock including waste plastics and / or waste rubber, comprising the steps of: a) introducing the feedstock into a fluidized bed gasifier using sand as a fluidizing medium; b) in the fluidized bed gasifier, under non-combustion conditions, contacting the feedstock introduced in step a) with a fluidized bed fluidized with atmospheric pressure superheated steam to thermally decompose it and generate a decomposition gas; and c) generating atmospheric pressure superheated steam in an atmospheric pressure superheated steam generator having a fluidized bed combustor using sand as a fluidizing medium and supplying it to the fluidized bed gasifier, and an apparatus for carrying out the method is provided.

Description

Technical Field

[0001] The present invention relates to a method for producing decomposed liquid and / or gaseous hydrocarbons from a feedstock containing waste plastics and / or waste rubber.

[0002] The present invention also relates to a pyrolysis gasification / oilification apparatus for producing decomposed liquid and / or gaseous hydrocarbons from a feedstock containing waste plastics and / or waste rubber.

Background Art

[0003] Generally, waste collected from households and factories contains various rubbers, plastics, or their mixed materials (hereinafter also referred to as plastics). Conventionally, as a recycling method for such plastics, various methods have been studied for decomposing waste plastics to obtain gas, fuel oil, or raw material oil for petrochemical products.

[0004] For example, Patent Document 1 describes a method of supplying waste plastics to a moving bed reactor and decomposing the plastics therein.

[0005] In addition, Patent Document 2 describes a pyrolysis process in which a thermoplastic is brought into contact with a fluidized bed of solid particles (generally sand) heated in an atmospheric pressure superheated steam atmosphere for melting and pyrolysis, and a regeneration process in which the solid particles from this process are heated in a fluid state to gasify the adhering combustibles, and both processes are carried out while circulating the solid particles between the two processes. In addition, in this process, since it is carried out in an atmospheric pressure superheated steam atmosphere, in addition to simple pyrolysis, hydrolysis also occurs in part.

[0006] However, there is still room for improvement in many aspects regarding the methods and equipment for the thermal decomposition and oil conversion of waste plastics as described above. For example, there is a need for methods and equipment that can achieve high safety and efficiency while also realizing high recyclability and low costs, especially in small-scale plants. Furthermore, it is desirable that such methods and equipment can also be used to thermally decompose and oil conversion waste rubber such as waste tires. For example, HIPS, used in tofu containers, is a polystyrene resin (PS) that has been mixed with rubber to enhance its impact resistance, and it is not possible to separate the rubber and plastic when disposing of it. [Prior art documents] [Patent Documents]

[0007] [Patent Document 1] Japanese Patent Application Publication No. 6-228569 [Patent Document 2] Japanese Patent Application Publication No. 59-111815 [Overview of the project] [Problems that the invention aims to solve]

[0008] The object of the present invention is to provide a method for producing decomposed liquid and / or gaseous hydrocarbons from supply materials including waste plastics and / or waste rubber, the method having high efficiency and / or high recyclability.

[0009] The present invention also aims to provide a highly safe method for producing decomposed liquid and / or gaseous hydrocarbons from supply materials including waste plastics and / or waste rubber. Most explosion and fire accidents in pyrolysis gasification furnaces occur when air enters the furnace or the ducts and tanks connected to it, and the mixture of air and gaseous hydrocarbons reaches a concentration between the lower and upper explosive limits. This occurs when some high-temperature heat source or ignition source (including electrostatic sparks) causes the mixture to exceed its flash point or ignition point. The pyrolysis furnace and surrounding flow paths and containers of the present invention are filled with atmospheric pressure superheated steam, and the partial pressure of oxygen required for explosion and ignition is kept far below the lower explosive limit, thus maintaining a low-oxygen state.

[0010] A further object of the present invention is to provide a pyrolysis gasification / oil conversion apparatus, particularly a small-scale pyrolysis gasification / oil conversion apparatus, for producing decomposed liquid and / or gaseous hydrocarbons from feedstock including waste plastics and / or waste rubber under atmospheric pressure (or under atmospheric pressure and partially reduced pressure). In this context, "small-scale" refers to a system where each pyrolysis furnace processes approximately 10 tons or less of plastic per day.

[0011] Other objects of the present invention will become apparent from the following description. [Means for solving the problem]

[0012] This invention has been made in view of the above-mentioned conventional technical problems, and relates, for example, to the following: 1. A method for producing decomposed liquid and / or gaseous hydrocarbons from supply materials including waste plastics and / or waste rubber, a) A step of introducing the supply material into a fluidized bed gasifier using sand as a fluidizing medium, b) In the fluidized bed gasifier, under non-combustion conditions, the supply material introduced in step a) is brought into contact with a fluidized bed that has been fluidized with superheated steam at atmospheric pressure to thermally decompose it and generate a decomposition gas. c) A step of generating atmospheric pressure superheated steam in an atmospheric pressure superheated steam generator having a fluidized bed combustor using sand as a fluidizing medium, and supplying this to the fluidized bed gasifier in step b) in order to fluidize the fluidized bed of the fluidized bed gasifier, d) A step of separating the decomposition gas produced in step b) in a distillation column to recover the oil, and e) A step in which at least a portion of the fluidized sand containing residual combustible material generated in the fluidized bed gasifier in step b) is supplied to the fluidized bed combustor of the atmospheric pressure superheated steam generator, and the residual combustible material is burned as at least a portion of the fuel for generating atmospheric pressure superheated steam in step c), including, and The method wherein steps a) to c) and e) are performed under normal pressure. 2. Follow these steps: f) A step of returning the fluidized sand generated after burning the residual combustible material in step e) to the fluidized bed gasifier, The method described in item 1 above, further comprising: 3. The method according to 2, wherein in step f), the fluidized sand is added to the supply material introduced in step a) and returned to the fluidized bed gasifier. 4. The method according to any one of 1 to 3 above, wherein the supply raw material introduced in step a) further comprises a chlorine abatant and / or a sulfur abatant, and / or an FCC catalyst. 5. The method according to any one of 1 to 4 above, wherein in step a), the supply material is introduced into the fluidized bed through the side wall of the fluidized bed gasifier at an upward gradient by a screw feeder, which has a screw shaft inserted into a cylindrical casing. 6. The method according to item 5 above, wherein the gradient angle of the upward slope is 10 to 35°. 7. The method according to any one of 1 to 6 above, wherein the separation of the decomposition gas in step d) is performed using a multi-stage vacuum distillation column. 8. The method according to any one of 1 to 7 above, wherein the residual oil produced in the distillation column in step d) is heated, and at least a portion of the residual oil thermal decomposition product obtained thereby is returned to the distillation column. 9. The method according to any one of 1 to 8 above, wherein propane is obtained by the separation of the decomposition gas in step d), and the propane is also supplied to the atmospheric pressure superheated steam generator and used as part of the fuel for generating atmospheric pressure superheated steam. 10. The method according to any one of 1 to 9 above, wherein in step b), the blowing velocity of the atmospheric pressure superheated steam used to fluidize the fluidized bed is 1 m / second or less. 11. The method according to any one of the above 1 to 10, wherein step b) is performed at a furnace temperature of 250 to 400°C. 12. The method according to any one of the above 1 to 11, wherein the amount of decomposition gas produced from step b) is 10 tons or less per day. 13. A method according to any one of the above 1 to 12, performed in a continuous manner. 14. A pyrolysis gasification / oil conversion apparatus for producing decomposed liquid and / or gaseous hydrocarbons from feedstock containing waste plastics and / or waste rubber, - A fluidized bed gasifier adapted to include a fluidized bed with sand as the fluidizing medium, which is fluidized by atmospheric pressure superheated steam at atmospheric pressure and brought into contact with the supply material under non-combustion conditions to generate decomposition gas. - A supply device that supplies the raw material to the fluidized bed gasifier at atmospheric pressure. - A distillation column to which the decomposition gas produced in the fluidized bed gasifier is sent, and to which the decomposition gas is separated under atmospheric or reduced pressure to recover oil, and - An atmospheric pressure superheated steam generator that supplies atmospheric pressure superheated steam to the fluidized bed gasifier at atmospheric pressure. Includes, The atmospheric pressure superheated steam generator is a fluidized bed combustor that burns fuel for generating atmospheric pressure superheated steam, and includes a fluidized bed combustor to which at least a portion of the spent fluidized sand produced in the fluidized bed gasifier is sent. The aforementioned device. 15. The apparatus according to 14, wherein the fluidized bed combustor is configured to return at least a portion of the fluidized sand in the fluidized bed combustor to the fluidized bed gasifier. 16. A fluidized sand recovery line for extracting at least a part of the used fluidized sand from the fluidized bed gasifier and supplying it to the fluidized bed combustor, and a fluidized sand return line for extracting at least a part of the fluidized sand in the fluidized bed combustor and returning it to the fluidized bed gasifier, wherein the fluidized sand return line is connected to the fluidized bed gasifier via the supply device. The apparatus according to item 15 above. 17. The supply device is a screw feeder having a screw shaft inserted into a cylindrical casing, and the screw feeder is connected to the fluidized bed gasifier with an upward gradient. The apparatus according to any one of items 14 to 16 above. 18. The gradient angle of the upward gradient is 10 to 35°. The apparatus according to item 17 above. 19. The supply device further includes a hopper adapted to be able to introduce the feedstock, the fluidized sand for the fluidized bed gasifier, and optionally a chlorine and / or sulfur scavenger, and / or optionally an FCC catalyst together into the screw feeder. The apparatus according to item 17 or 18 above. 20. The distillation column is connected to the atmospheric pressure superheated steam generator so that the propane obtained therein can be supplied to the atmospheric pressure superheated steam generator. The apparatus according to any one of items 14 to 19 above. 21. The apparatus according to any one of items 14 to 20 above, further comprising an oil bath having a heater between the fluidized bed gasifier and the distillation column or at the bottom of the distillation column. 22. The apparatus according to any one of items 14 to 21 above, wherein the amount of decomposition gas generated in the fluidized bed gasifier is a small-scale device of 10 t or less per day. 23. The apparatus according to any one of items 14 to 22 above, which is a continuous device. 24. The fluidized bed combustor includes an air inlet. The apparatus according to any one of items 14 to 23 above. 25. The apparatus according to any one of items 14 to 24 above, for implementing the method according to any one of items 1 to 13 above.

[0013] By using the method and apparatus of the present invention, waste plastics and / or waste rubbers can be gasified and / or liquefied with high efficiency while ensuring high safety. Furthermore, in this invention, residual combustible material from the gasification furnace is sent together with fluidized sand to the fluidized bed combustor of an atmospheric pressure superheated steam generator and used as fuel for combustion in the combustor. This allows the heat required for generating atmospheric pressure superheated steam to be supplied, thus achieving energy savings and cost reduction. Moreover, the present invention provides a method and apparatus particularly suitable for miniaturization of the apparatus. [Modes for carrying out the invention]

[0014] In one embodiment of the present invention, the present invention relates to a pyrolysis gasification / oil conversion apparatus for producing decomposed liquid and / or gaseous hydrocarbons from a feedstock including waste plastics and / or waste rubber.

[0015] The above apparatus and method will be described below with reference to the drawings.

[0016] Figure 1 is a scheme diagram showing an exemplary embodiment of the pyrolysis gasification / oil conversion apparatus and method of the present invention (for a raw material input of 400 kg / h). The pyrolysis gasification / oil conversion apparatus 1 shown in Figure 1 comprises a fluidized bed gasifier 2, a supply device 4, a distillation column 5, and an atmospheric pressure superheated steam generator 6.

[0017] The above apparatus can obtain (decomposed) liquid and / or gaseous hydrocarbons by thermally decomposing and gasifying the waste plastics and / or waste rubber contained in the supply raw materials, and then converting them into oil. The apparatus can be operated entirely under atmospheric pressure, or under atmospheric pressure and partially under reduced pressure; for example, the distillation column 5 (and oil bath 55) can be operated under reduced pressure, while the rest can be operated under atmospheric pressure.

[0018] The apparatus 1 described above includes a fluidized bed gasifier 2 adapted to include a fluidized bed 3 in which sand is used as a fluidizing medium, which is fluidized by atmospheric pressure superheated steam at atmospheric pressure and brought into contact with the supply raw material under non-combustion conditions to generate decomposition gas.

[0019] The sand in the fluidized bed 3 is fluidized at atmospheric pressure by atmospheric pressure superheated steam, and the feed material introduced into the fluidized bed gasifier 2 is brought into contact with it under non-combustion conditions, thereby heating and decomposing the feed material and generating decomposition gas. The fluidized bed gasifier 2 is equipped with the fluidized bed 3 at least when in operation, but may or may not be equipped with the fluidized bed 3 when not in operation; that is, the fluidized bed gasifier 2 may or may not be filled with sand as a fluidized bed. In this context, such a configuration is expressed as the fluidized bed gasifier 2 being "adapted to be equipped with (as described above) a fluidized bed 3". This also applies to the fluidized bed combustor 7 (fluidized bed 8).

[0020] Here, non-combustion conditions mean conditions under which the supply material, including organic waste such as waste plastics and waste rubber, does not undergo a combustion reaction. In other words, it means that there is no oxygen in the fluidized bed gasifier 2, or the oxygen concentration in the furnace is below the oxygen concentration (limiting oxygen concentration) at which the supply material undergoes a combustion reaction (a low oxygen atmosphere). For example, the oxygen concentration can be less than 1.0%, more preferably less than 0.4%, and particularly preferably 0.1% or less.

[0021] By thermally decomposing waste plastics and waste rubbers, which are used as raw materials for oil conversion, under non-combustion conditions in a fluidized bed using a superheated steam heat source at atmospheric pressure, organic gases (decomposition gases) can be obtained. Since organic matter is being gasified, the presence of oxygen could cause an explosion. However, by introducing superheated steam at atmospheric pressure, the furnace is filled with superheated steam, and the oxygen concentration is extremely low. Therefore, even if organic gases are generated, an explosive mixture is not created, and the oxygen-free thermal decomposition reaction can occur safely.

[0022] Furthermore, because it uses superheated steam at atmospheric pressure, i.e., steam, it has the advantage that even if water-soluble harmful substances are generated, they can be dissolved and removed as an aqueous solution. For example, in the case of hydrogen chloride, it can be separated and removed from the furnace as hydrochloric acid.

[0023] The aforementioned thermal decomposition can be carried out at a furnace temperature of 250 to 700°C, preferably 300 to 600°C, and more preferably 430 to 550°C (preferably the gas temperature of the free board section). For example, the thermal decomposition can be carried out at a furnace temperature of 250 to 400°C.

[0024] Here, the fluidizing medium for the fluidized beds (fluidized bed 3 and fluidized bed 8) can be silica sand, river sand, foundry sand, power plant ash, brick waste, glass granules, and slag particles produced as reaction residues in the fluidized bed furnace, or a mixture thereof can be used (in this specification, such fluidizing mediums for fluidized beds are collectively referred to simply as "sand" or "fluidized sand"). That is, in the present invention, in a fluidized bed which is an aggregate of solid fine particles suspended in a gaseous state, the above-mentioned "sand" can be mainly used as the solid fine particles. Preferably, silica sand (or sand mainly containing silica sand, for example, sand substantially composed of silica sand) is used as the fluidizing medium. The particle size of the fluidizing medium is not particularly limited as long as the fluidized bed is properly fluidized, but for example, a fluidizing medium having a particle size of 2 mm or less, preferably 0.5 mm or less, for example, 100 to 500 μm can be used. The blowing velocity / flow rate of the atmospheric pressure superheated steam used to fluidize the fluidized bed is preferably set so that the fluidized sand is not blown upwards. The aforementioned blowing velocity / flow rate can be 2 m / sec or less, generally 1 m / sec or less, depending on the particle size of the fluid medium, and can be, for example, 0.05 m / sec to 1.5 m / sec, or 0.1 to 1 m / sec. Such a blowing velocity / flow rate allows the fluid medium to flow uniformly while preventing excessive blowing.

[0025] In one embodiment of the present invention, pyrolysis in a fluidized bed gasifier 2 can be carried out in the presence of an FCC (fluid-contact) catalyst. The FCC catalyst can be introduced into the fluidized bed 3, where it exists together with sand, preferably mixed with sand. It has been found that using the FCC catalyst in the gas phase allows it to exhibit and maintain higher reactivity than when used in the liquid phase, decomposing gasified high-molecular-weight organic substances, suppressing the production of poor quality heavy oil, and improving the yield of light oil, kerosene, naphtha, etc. By promoting pyrolysis of components that become heavy oil after pyrolysis as much as possible and converting them into smaller molecules (light oil), the generation of heavy oil and tar that harden at room temperature can be reduced. Furthermore, high temperatures are required to decompose substances with strong intermolecular forces, such as benzene rings, by pyrolysis, but if the temperature is too high, cracking occurs, which can adversely affect the quality of the resulting oil. By using such a catalyst, the temperature required to achieve pyrolysis can be reduced, making it possible to ensure both the achievement of pyrolysis and the good quality of the resulting oil.

[0026] The FCC catalyst is not particularly limited as long as it is a catalyst that can be used in the fluid catalytic cracking (FCC) process. Such FCC catalysts are well known and various types are commercially available. For example, catalysts composed of clay such as zeolite, activated alumina, silica gel, and kaolin can be used, and for example, granular (e.g., particle size of 10-100 μm) or pelletized (synthetic) zeolite-based catalysts can be used.

[0027] The FCC catalyst can be introduced into the fluidized bed 3 of the fluidized bed gasifier 2 separately from the supply raw materials, but preferably, it is introduced into the fluidized bed 3 of the fluidized bed gasifier 2 from the supply device 4 together with the supply raw materials, and more preferably in a mixed state with the supply raw materials.

[0028] In one embodiment of the present invention, the method can be carried out in the presence of a detoxifying agent that chemically reacts with harmful components and renders them harmless (typically by decomposing them or converting them into harmless forms). The detoxifying agent is not particularly limited as long as it can render / remove harmful components, especially chlorine and / or sulfur, but is preferably a chlorine detoxifying (chlorine removal) and / or sulfur detoxifying (sulfur removal) agent, i.e., a chlorine detoxifying agent and / or sulfur detoxifying agent, for example, a dry detoxifying agent. For example, the detoxifying agent is selected from the group consisting of calcium hydroxide, calcium carbonate, calcium oxide, sodium hydroxide, sodium bicarbonate, and potassium hydroxide. Particularly preferably, the detoxifying agent is calcium carbonate. The detoxifying agent may be, for example, crushed shells such as oyster shells or scallop shells.

[0029] For example, if waste plastic contains PVC (polyvinyl chloride), the fluidized bed gasifier 2 generates HCl (hydrogen chloride) gas, which is a toxic gas, through thermal decomposition and gasification. If calcium carbonate is used as a detoxifier, the HCl is converted to CaCl2 (calcium chloride) through the following reaction and becomes harmless. 2HCl + CaCO3 → CaCl2 (harmless) + CO2 + H2O [Reaction Equation 1]

[0030] If waste rubber is included in the raw materials, even if calcium carbonate is used as a detoxifier, the sulfur (S) contained in the rubber will not react with calcium carbonate in the atmospheric pressure superheated steam atmosphere (non-combustion conditions) of the fluidized bed gasifier 2. However, the S will remain discharged from the fluidized bed gasifier 2 (for example, from the bottom) along with ash, sand, etc., and will be oxidized in the fluidized bed combustor 7 within the atmospheric pressure superheated steam generator 6, and can be detoxified by the following reaction. 2S + 3O2 + 2CaCO3 → 2CaSO4 (harmless) + 2CO2 [Reaction Equation 2] 2S + 2O2 + 2CaCO3 → 2CaSO3 (harmless) + 2CO2 [Reaction Equation 3] Calcium sulfate (CaSO4) is what is commonly known as "gypsum," and calcium sulfite (CaSO3) is also a harmless ceramic used for limescale removal and other purposes.

[0031] In this way, harmful substances (chlorine and sulfur) contained in polyvinyl chloride (PVC) and rubber can be neutralized using two types of fluidized beds (fluidized bed 3 of the fluidized bed gasifier 2 and fluidized bed 8 of the fluidized bed combustor 7) and a detoxifying agent (preferably calcium carbonate) while proceeding with the thermal decomposition and gasification of plastics and rubber.

[0032] For example, the detoxifying agent can be introduced separately from the supply raw materials into the fluidized bed gasifier 2 (fluidized bed 3) and / or into the fluidized bed combustor 7 (fluidized bed 8) in the atmospheric pressure superheated steam generator 6, but preferably it is introduced together with the supply raw materials, more preferably in a mixed state with the supply raw materials, from the supply device 4 into the fluidized bed 3 of the fluidized bed gasifier 2.

[0033] The aforementioned raw materials (waste plastics and waste rubber as oil-converting raw materials) are preferably introduced into the fluidized bed gasifier 2 together with fluidized sand and optionally an FCC catalyst and / or a detoxifier. For example, a mixture of these materials can be prepared in advance by mixing them in a predetermined ratio, and then fed into the fluidized bed 3 of the fluidized bed gasifier 2 using a supply device 4 (e.g., a screw feeder) without changing the mixing ratio. The mixing ratio can be appropriately set by those skilled in the art depending on the raw materials.

[0034] The apparatus 1 described above includes a supply device 4 that can supply the raw material to the fluidized bed gasifier at atmospheric pressure.

[0035] In one embodiment of the present invention, the raw material is introduced into a fluidized bed gasifier 2 via a supply device 4. The supply device 4 is not particularly limited as long as it can introduce the raw material into the fluidized bed gasifier 2 in a desired amount, for example, continuously or intermittently. Examples of the supply device 4 include a screw feeder, a vibratory feeder, a rotary feeder, a belt feeder, and the like. For example, when using a screw feeder, the amount of raw material supplied to the fluidized bed gasifier 2 can be controlled by adjusting the rotation speed of the screw, or, for example, when using a vibratory feeder, by adjusting the vibration frequency, amplitude, etc.

[0036] In a preferred embodiment of the present invention, a screw feeder 12 is used as the supply device 4. A known screw feeder can be used, and typically a screw feeder has a screw shaft, on which extrusion blades are helically attached to the outer circumference of the rotating shaft, rotatably inserted into a cylindrical casing. The screw feeder makes it possible to feed the raw material into the fluidized bed gasifier 2, preferably by pressurization. In a more preferred embodiment of the present invention, the screw feeder 12 is connected to the fluidized bed gasifier at an upward slope. This makes it possible to introduce the raw material into the fluidized bed at an upward slope through the side wall of the fluidized bed gasifier by the screw feeder.

[0037] When a supply device, such as a screw feeder, is used horizontally, the lower half of the casing is transported in a dense state, fully filled with the supply material, while a gap forms in the upper half, allowing outside air (containing oxygen) to conduct through. In such cases, oxygen can enter the furnace along with the supply material, making it impossible to maintain non-combustion conditions. However, as described above, by feeding the supply material into the sand layer of the fluidized bed of a fluidized bed gasifier using an upward-sloping screw feeder, the inside of the screw feeder casing can be filled with particles of the supply material (and optionally sand, aerosols, and / or FCC catalyst), preventing outside air (containing oxygen) from conducting through the supply device (e.g., screw feeder) into the furnace. Therefore, even when the fluidized bed is under negative pressure, outside air can be prevented from entering the furnace. This configuration makes it possible to strictly maintain non-combustion conditions, and thus it has been found to be extremely advantageous from a safety standpoint.

[0038] Regarding the above-mentioned gradient, a certain gradient angle is necessary to enjoy the above-mentioned advantages. However, if the gradient angle is too large, the length of the screw feeder in the mechanical direction (direction of feed material travel) will generally be shortened, reducing the amount of space that can be blocked by the feed material and shut off from the outside air. Furthermore, depending on the particle size of each particle in the feed material (and optionally sand, abatants, and / or FCC catalyst), some material (typically larger particle size material) will be transported by the screw feeder and reach the furnace, while other material (typically smaller particle size sand, etc.) will fall down the slope of the screw feeder without being transported, resulting in gaps that may allow outside air to enter. In this case, even if the feed material has been prepared in advance considering the mixing ratio of each component, the mixing ratio may have changed by the time the material is introduced into the furnace. In this application, it was also found that non-combustion conditions can be optimally maintained when the gradient angle (the angle of the screw rotation axis of the screw feeder relative to the horizontal) is 5 to 40°, preferably 10 to 35°, and more preferably 12 to 30°.

[0039] Accordingly, in one embodiment of the present invention, the supply device is a screw feeder in which a screw shaft is inserted into a cylindrical casing, and the screw feeder is connected to the fluidized bed gasifier with an upward slope. Furthermore, in a further embodiment of the present invention, the slope angle of the upward slope is 10 to 35°.

[0040] In one embodiment of the present invention, the supply device comprises a hopper 11 in addition to the screw feeder. The hopper 11 is adapted to allow the supply material and, optionally, fluidized sand for the fluidized bed gasifier, chlorine and / or sulfur abatants, and / or FCC catalysts to be introduced together.

[0041] In one embodiment of the present invention, the supply material is fed into a hopper 11 and then supplied from there to a screw feeder 12. For example, the hopper 11 is connected to one end of the screw feeder 12 (the supply material inlet of the screw feeder 12), and the other end of the screw feeder 12 (the supply material outlet to the fluidized bed gasifier 2) is connected to the fluidized bed gasifier 2. When the supply material is fed into the hopper 11, the hopper 11 supplies the supply material to the screw feeder 12, preferably in required amounts, and as described above, the screw feeder 12 supplies it to the fluidized bed gasifier 2 through the side wall of the fluidized bed gasifier. A known hopper can be used as the hopper 11. For example, the hopper 11 has a wide-mouthed material inlet formed at the top of the hopper body and an opening at the bottom of the body that leads to the supply material inlet of the screw feeder 12.

[0042] Preferably, the raw material is fed into the supply device 4 (preferably hopper 11) together with fluidized sand, preferably after being mixed / blended with fluidized sand. That is, the raw material can be fed into the supply device 4 together with (preferably mixed with) the sand used for the fluidized bed 3 of the fluidized bed gasifier 2 and / or the sand returned from the fluidized bed 8 of the fluidized bed combustor 7. Some waste plastics and waste rubber contained in the raw material may have large particle sizes or be bulky, and if such material is put directly into the supply device 4 (hopper 11), gaps may form and gas may escape. However, by putting it together with sand, the gaps can be filled, thus maintaining the airtightness of the raw material and, consequently, maintaining non-combustion conditions in the fluidized bed gasifier 2. In a preferred embodiment of the present invention, from the viewpoint of improving and maintaining the airtightness, sand is added to the fluidized bed gasifier 2 together with the raw material as needed, preferably continuously (during operation). When using a detoxifying agent and / or an FCC catalyst, preferably the raw material is mixed / blended with the fluidized sand and the detoxifying agent and / or FCC catalyst before being supplied to the supply device 4 (preferably hopper 11). The mixing ratio of the raw material and sand can be adjusted as appropriate, taking into account the airtightness of the raw material. For example, the mixing may be performed by a mixer, and such a mixer is not particularly limited as long as it can properly mix the raw material and sand, etc. For example, the raw material can be supplied to the apparatus 1 by putting the raw material and sand (and optionally the detoxifying agent and / or FCC catalyst) into a mixer and transferring the resulting mixture / blend to hopper 11.

[0043] Thus, the supply device 4 may include a hopper 11 for introducing the supply material, and optionally fluidized sand, chlorine and / or sulfur decontaminants, and / or FCC catalyst for the fluidized bed gasifier, together into the screw feeder 12.

[0044] In large-scale industrial complexes and similar facilities, raw materials are typically supplied to separate hoppers for each material. However, as described above, the pyrolysis gasification / oil conversion apparatus 1 of the present invention is preferably a small-scale apparatus. By pre-mixing the raw materials, sand, abatants, FCC catalyst, etc., and feeding them into a single hopper, the number of hoppers can be reduced, thereby miniaturizing the supply device configuration; in other words, a supply device with only one hopper can be used. Therefore, pre-mixing of the raw materials contributes to the miniaturization of the apparatus. Accordingly, in one embodiment of the present invention, the supply device comprises one hopper (i.e., a single hopper). For example, in one embodiment, the apparatus 1 includes one supply device 4, and the supply device 4 may comprise a single hopper 11. Furthermore, the pre-mixing of the raw materials can be performed at a location different from the operating location of the apparatus 1, and the resulting mixture / blend may be transported to the apparatus 1 and fed into the supply device (preferably hopper 11). Because pre-mixed raw materials can be fed into a single hopper, operation is simple, and the operator does not need to have a high level of expertise to operate the equipment.

[0045] Furthermore, in the case of small-scale equipment, if separate desulfurization devices, dechlorination devices, and desalination devices are provided, their installation costs alone account for a large portion of the overall equipment cost. However, in the present invention, by introducing a toxic agent together with the supplied raw materials as described above, it becomes possible to detoxify harmful substances across two types of fluidized beds using the toxic agent, thus eliminating the need to arrange separate, independent devices as described above. Consequently, it is possible to provide particularly small-scale equipment while achieving significant cost reductions. Therefore, in one embodiment of the present invention, the pyrolysis gasification / oil conversion apparatus does not include separate desulfurization devices, dechlorination devices, and / or desalination devices.

[0046] The apparatus 1 described above includes a distillation column to which the decomposition gas generated in the fluidized bed gasifier is sent in order to recover oil, and which separates the decomposition gas under atmospheric or reduced pressure. The decomposition gas produced in the fluidized bed gasifier 2 is sent to the distillation column 5, where it is separated. The decomposition gas is supplied to the distillation column 5 by a decomposition gas supply line 13 that connects the fluidized bed gasifier 2 (preferably the part above the fluidized bed 3, especially the top of the column or its vicinity) and the distillation column 5 (preferably the bottom of the column). Here, the decomposition gas supply line can be, for example, a pipe, conduit, or piping, but it is not particularly limited in terms of material, shape, and diameter (inner diameter, outer diameter, etc.) as long as it can properly deliver the decomposition gas from the gasifier 2 to the distillation column 5. In the distillation column 5, the decomposition gas is separated into gas fraction, naphtha fraction, kerosene fraction, light oil fraction, heavy oil fraction, etc. by a method known to those skilled in the art, and thereafter, the desired oil can be recovered as appropriate according to a method known to those skilled in the art. For example, each fraction may be optionally sent to each fraction tank (22-25) by a fraction pump 27 after passing through a fraction condenser 26 connected to a distillation column for recovery. For example, each oil type can be separated into oil and water and shipped.

[0047] The distillation column 5 is operated under atmospheric pressure or reduced pressure. Preferably, a multi-stage distillation column is used as the distillation column 5, and more preferably, a multi-stage vacuum distillation column is used. In the distillation column 5, the gasification product is subjected to multi-stage condensation and separation distillation, making it possible to appropriately separate and recover each fraction.

[0048] For example, the gas fraction may be taken from the top of the column, while the other fractions are taken as a side-cut flow. For example, naphtha fraction, kerosene fraction, light oil fraction, and heavy oil fraction can be taken in order from the top in the middle of the column. The amount of each oil type and fraction produced may vary depending on the type and amount of raw materials, but can be, for example, 10-80 kg / h, 20-60 kg / h, or 25-55 kg / h.

[0049] In this way, decomposed liquid and / or gaseous hydrocarbons can be obtained from the feed material via the distillation column 5.

[0050] The oil produced by gasification and liquefaction is a mixture of naphthas (volatile oils: Class 1 petroleum) to solid oil components (ultra-heavy oils: Class 4 petroleum), and is not separated by oil type, thus limiting its uses. However, by processing in the distillation column 5 as described above, Class 2 and Class 3 petroleum can be separated and extracted, making it usable in internal combustion engines (mainly diesel engines). Oils with a pour point higher than room temperature (mainly Class 4 petroleum) are difficult to handle as liquid fuels, posing particular problems in storage, transportation, and use during winter, and also have low added value, so such components can also be removed.

[0051] Furthermore, the aforementioned gas fraction is typically a petroleum gas component (PG component) containing propane and butane, and can be used for generating atmospheric pressure superheated steam in atmospheric pressure superheated steam generators, as described later (it can also be used in burners for oil baths).

[0052] In one embodiment of the present invention, the apparatus 1 further includes an oil bath 55 equipped with a heater (preferably a combustor), which is placed between the fluidized bed gasifier 2 and the distillation column 5, or at the bottom of the distillation column 5.

[0053] Pyrolysis in the fluidized bed gasifier 2 is not always sufficient, and a large amount of molecules with high molecular weights and high carbon number molecules (for example, high-boiling-point hydrocarbons with 60 or more carbon atoms) remain. These components are also called "wax" and become solid oil at room temperature. In this invention, the decomposition gas from the fluidized bed gasifier 2 is sent to the distillation column, but at the same time, the pyrolysis gas in the process of pyrolysis, that is, the raw material for wax, is also carried into the distillation column by atmospheric pressure superheated steam. For example, in a multi-stage distillation column, the substances are distilled as liquids at each stage according to their boiling point through multi-stage gas-liquid contact, but the organic substances called wax components that have not been sufficiently pyrolyzed, as described above, have a boiling point that is too high and a vapor partial pressure that is too low, so they cannot rise up the trays and are not distilled, and continue to accumulate at the bottom of the distillation column as high-temperature residual oil (also called "heavy residual oil" or "residual heavy oil"). By providing an oil bath (oil tank) equipped with a heater (preferably a combustor), the heavy residue oil described above can be stored in the oil bath and heated there by the heater. Most of the heavy residue oil undergoes thermal decomposition upon heating, which lowers its molecular weight and boiling point, and increases its vapor partial pressure, allowing it to rise up the trays of the distillation column and become a fraction.

[0054] The oil bath 55 is a container having a certain volume in which the heavy residue oil can be stored. The oil bath 55 may also have an inlet for introducing a decomposition gas flow from the fluidized bed gasifier 2 and an outlet for sending the gas flow from the oil bath 55 to the distillation column. The oil bath 55 is equipped with a heater, for example, a combustor 37 (hereinafter also referred to as a "burner") for heating the heavy residue oil stored inside, and preferably the combustor is provided, for example, at the bottom of the oil bath (inside) so that at least a part of it is placed in the residue oil liquid stored in the oil bath. The heater (preferably a burner) is not particularly limited in its configuration as long as it can sufficiently heat the residue oil stored in the oil bath. For example, as shown in Figure 1, a burner can be used which is configured such that the combustion gas comes into contact with the residue oil via a radiant tube.

[0055] As fuel for the burner, for example, at least a portion of the off-gas (typically the PG gas mentioned above) that does not condense even when it rises to the top of the distillation column, or at least a portion of the heavy residue oil accumulated in the oil bath can be taken out and used. In this case, the burner will inevitably be a burner that co-fires gaseous and liquid fuels.

[0056] Furthermore, even in an oil bath 55 like this one, heavy residual oil (waste oil) that has not been thermally decomposed can be burned in a burner and used as a heat source. Heavy residual oil is a solid oil at room temperature and is classified as a Class 4 petroleum product under the Fire Service Act. While there are few restrictions on storage, it has a high calorific value (approximately 10,000 kcal / kg: HHV (Higher Heating Value)), making it quite valuable as a solid fuel. In particular, oil sands, which are oil sands mixed with sand, can be used as fuel for stable high-temperature flames in fluidized bed combustors and kiln combustors. However, since sand is non-combustible, oil sands fuel has a low calorific value per unit weight (less than half of the HHV value mentioned above).

[0057] In this application, it has been found that by providing an oil bath 55 as described above, it is possible to reduce high-boiling-point hydrocarbons with a large number of carbon atoms (for example, C60 or more), and consequently, to homogenize the recovered oil product.

[0058] The oil bath can take the form of a tank, for example. However, the oil bath is not particularly limited as long as it can provide a space inside, preferably at the bottom (e.g., the lower part), that can sufficiently store heavy residue oil while allowing the decomposition gas (gaseous component) from the fluidized bed gasifier 2 to pass through successfully without being affected by the presence of the accumulated heavy residue oil (typically passing over the accumulated residue oil).

[0059] As described above, the oil bath 55 is located between the fluidized bed gasifier 2 and the distillation column 5, or at the bottom of the distillation column 5. The oil bath 55 may be connected to the fluidized bed gasifier 2 and the distillation column 5 via the decomposition gas supply line 13, or it may be connected directly without the decomposition gas supply line 13. For example, it may be connected to one of the fluidized bed gasifier 2 and the distillation column 5 via the decomposition gas supply line 13, and to the other directly.

[0060] As described above, residual oil is stored inside the oil bath 55, but typically the oil bath 55 is not filled with residual oil throughout its entire internal space. For example, there are spaces at the top or apex that are not filled with residual oil. The inlet and outlet of the oil bath 55 can be provided separately at locations that lead to spaces not filled with residual oil (for example, the top of the oil bath container, especially the apex). In one embodiment of the present invention, a decomposition gas supply line 13 from a fluidized bed gasifier 2 is connected to the inlet of the oil bath 55, thereby introducing decomposition gas from the fluidized bed gasifier 2 into the oil bath 55. The bottom of a distillation column 5 is directly connected to the outlet of the oil bath 55, and the decomposition gas is sent directly to the distillation column 5 from there. Meanwhile, heavy residue oil is stored in the oil bath, but a portion of it is converted into hydrocarbons with fewer carbon atoms after heating by a burner and sent to the distillation column 5 together with the decomposition gas. Here, the oil bath 55 may be integrated with the distillation column 5. Alternatively, the oil bath 55 may be integrated with both the decomposition gas supply line 13 from the fluidized bed gasifier 2 and the distillation column 5.

[0061] As described above, the oil bath can be, for example, a tank, but its material, shape, volume, size, etc., are not particularly limited, as long as it can store a sufficient amount of heavy residue oil while allowing the decomposition gas from the fluidized bed gasifier 2 to pass through directly.

[0062] In a further embodiment of the present invention, the oil bath 55 may contain a catalyst, preferably an FCC catalyst, for example, in the form of a catalyst bed. As described above, the decomposition gas from the fluidized bed gasifier 2 may contain organic matter called wax components that are not sufficiently decomposed by thermal decomposition, and such components continue to accumulate at the bottom of the distillation column as high-temperature heavy residue oil. However, by supplying the decomposition gas to the distillation section via the oil bath 55 as described above, the decomposition gas is supplied directly to the distillation column, while the wax components remain in the oil bath as heavy residue oil for a sufficient reaction time, and the catalyst in the oil bath breaks particularly long chain C=C bonds, converting them into hydrocarbons with a reduced number of carbon atoms. Because these hydrocarbons with shortened carbon chains are lighter, they rise and are sent to the distillation column, where they ascend the trays and become fractions. By including such a catalyst, it is possible to further reduce the amount of wax components and achieve even greater homogenization of the recovered oil product.

[0063] In a preferred embodiment, the pyrolysis gasification / oil conversion apparatus 1 of the present invention is miniaturized, and therefore the distillation column 5 included therein is also a small distillation column. While petrochemical complexes and refineries have a scale of 300,000 barrels (approximately 50,000 tons) per day, the processing capacity (amount of decomposition gas subjected to processing) of the distillation column 5 in the present invention is preferably 10 tons or less per day.

[0064] The apparatus 1 described above includes an atmospheric pressure superheated steam generator that supplies atmospheric pressure superheated steam to the fluidized bed gasifier at atmospheric pressure. The atmospheric pressure superheated steam generator 6 generates atmospheric pressure superheated steam, which is then supplied to the fluidized bed gasifier 2. Here, the atmospheric pressure superheated steam generator 6 is equipped with a fluidized bed combustor 7 that uses sand as a fluidizing medium, and the heat generated by burning fuel in the fluidized bed 8 within the fluidized bed combustor 7 is used as a heat source for generating atmospheric pressure superheated steam.

[0065] Generally speaking, superheated steam refers to water vapor (gas) heated above its boiling point. However, in fields dealing with steam boilers, it often refers to dry steam obtained by further increasing the temperature of pressurized saturated steam by adding sensible heat. However, the apparatus and method of the present invention require only high-temperature, dry superheated steam, and the pressure is preferably atmospheric pressure. Such atmospheric pressure superheated steam used in the present invention is called "atmospheric pressure superheated steam," and its generating device does not fall under the definition of "boiler" or "pressure vessel" as defined by the Industrial Safety and Health Act and the High-Pressure Gas Safety Act.

[0066] The configuration of the atmospheric pressure superheated steam generator 6 is not particularly limited, except that it operates under atmospheric pressure and uses the heat generated in a fluidized bed combustor 7, which uses sand as a fluidizing medium, as a heat source for generating atmospheric pressure superheated steam.

[0067] In one embodiment of the present invention, the atmospheric pressure superheated steam generator 6 comprises a fluidized bed combustor 7, an evaporator 16, and a superheater 17. Water supplied from a pure water tank 19 is heated by the evaporator 16 to generate steam, which is then supplied to the superheater 17 through a steam supply line 20. The steam supply line can be, for example, a pipe, conduit, or piping, but is not particularly limited in terms of material, shape, and diameter (inner diameter, outer diameter, etc.) as long as it can adequately deliver steam from the evaporator 16 to the superheater 17. The superheater 17 is in contact with the fluidized bed combustor 7 so as to be able to exchange heat, and the heat generated in the fluidized bed combustor 7 superheats the supplied steam to produce atmospheric pressure superheated steam. All of this is done under atmospheric pressure, and therefore atmospheric pressure superheated steam is produced. This atmospheric pressure superheated steam is superheated to a temperature such that the temperature in the fluidized bed gasifier 2, to which it is supplied, becomes the desired reaction temperature as described above. Preferably, atmospheric pressure superheated steam is supplied to the fluidized bed gasifier 2 at a temperature of 400 to 650°C, more preferably 450 to 600°C, for example, 500 to 580°C or 530 to 570°C.

[0068] The atmospheric pressure superheated steam generated in the atmospheric pressure superheated steam generator 6 can be supplied to the fluidized bed 3 of the fluidized bed gasifier 2 through the atmospheric pressure superheated steam supply line 18 connecting the atmospheric pressure superheated steam generator 6 and the fluidized bed gasifier 2. Here, the atmospheric pressure superheated steam supply line can be, for example, a pipe, conduit, or piping, but it is not particularly limited in terms of material, shape, or diameter (inner diameter, outer diameter, etc.) as long as it can appropriately deliver atmospheric pressure superheated steam from the atmospheric pressure superheated steam generator 6 to the fluidized bed gasifier 2.

[0069] The aforementioned atmospheric pressure superheated steam generator is a fluidized bed combustor that uses sand as a fluid medium to burn fuel for generating atmospheric pressure superheated steam, and includes a fluidized bed combustor to which at least a portion of the spent fluidized sand generated in the fluidized bed gasifier (this sand contains a large amount of residual organic matter that was not gasified, such as carbon particles, sludge, and coal tar, and these can also be used as fuel. Hereafter, these organic matter mixed in the spent fluidized sand will also be called "residual combustible matter") is sent. In the present invention, organic matter and the like (residual combustible matter) that remains on the fluidized sand side without being gasified during the thermal decomposition of the supply raw material in the fluidized bed gasifier 2 is used as at least a portion of the fuel for the fluidized bed combustor 7 of the atmospheric pressure superheated steam generator 6 and burned. For this reason, the fluidized bed combustor 7 is configured to receive at least a portion of the spent fluidized sand generated in the fluidized bed gasifier 2. For example, the pyrolysis gasification / oil conversion apparatus 1 includes a fluidized sand recovery line 9 connecting the fluidized bed 3 of the fluidized bed gasifier 2 and the fluidized bed combustor 7 of the atmospheric pressure superheated steam generator 6. The fluidized sand recovery line 9 can extract at least a portion of the spent fluidized sand from the fluidized bed gasifier 2 (e.g., the bottom) and supply it as fuel to the fluidized bed combustor 7 (fluidized bed 8). The spent fluidized sand is transported through the fluidized sand recovery line 9, but in one embodiment of the present invention, this transport can also be performed by pushing and discharging the spent fluidized sand from the fluidized bed 3 using a powered fluidized sand discharge device 15, preferably a screw conveyor, which is provided at the bottom of the fluidized bed gasifier 2 to connect the fluidized bed 3 and the fluidized sand recovery line 9. Here, the fluidized sand recovery line 9 can be, for example, a pipe, conduit, piping, or transport system, but it is not particularly limited in terms of material, shape, or diameter (inner diameter, outer diameter, etc.) as long as it can appropriately transport the used fluidized sand from the fluidized bed gasifier 2 to the fluidized bed combustor 7. Alternatively, a fluidized sand discharge device 15, preferably a screw conveyor, may function as the fluidized sand recovery line 9. In other words, the entire fluidized sand recovery line 9 may consist of a fluidized sand discharge device 15, preferably a screw conveyor. Such a screw conveyor can be one known to those skilled in the art and may have a structure similar to the screw feeder described above. As described above, during operation (or after operation), the fluidized bed in the fluidized bed gasifier 2 contains fluidized sand that includes and / or is mixed with residual combustible material. Therefore, at least a portion of this fluidized sand is discharged and supplied to the fluidized bed combustor 7. This fluidized sand (and the residual combustible material it contains) is also used as fuel in the fluidized bed combustor 7 and is preferably circulated and used within the apparatus 1. Therefore, it has not been used up in the entire apparatus 1, but from the perspective that its use in the fluidized bed gasifier 2 has been completed, in this application it is also referred to as "used" fluidized sand. Furthermore, a portion of the spent fluidized sand removed from the fluidized bed gasifier 2 may be used as fuel for the fluidized bed combustor 7 as described above, and the remainder (or a portion of the remainder) may be used as fuel for other heat sources.

[0070] Thus, in the fluidized bed combustor 7, fuel present with fluidized sand, typically fuel mixed with fluidized sand, is burned in a fluidized bed 8 that uses sand as the fluidizing medium. The fluidized bed 8 of the fluidized bed combustor 7 can use fluidizing mediums (such as silica sand) as described for the fluidized bed 3 of the fluidized bed gasifier 2, and can be operated at the blowing velocity / flow rate described for the fluidized bed 3.

[0071] However, in contrast to the fluidized bed gasifier 2, combustion in the fluidized bed combustor 7 takes place in the presence of air. Therefore, in one embodiment of the present invention, the fluidized bed combustor 7 is equipped with an air inlet from which combustion air is introduced into the fluidized bed combustor 7. Preferably, the air is preheated, for example, in a recuperator (exhaust heat recovery air preheater) and then preheated to, for example, 300 to 500°C, preferably 350 to 450°C, more preferably 380 to 420°C before being supplied into the sand layer at the bottom of the combustor. In one preferred embodiment of the present invention, the fluidized bed combustor 7 is equipped with a preheated air inlet for introducing preheated air.

[0072] In the atmospheric pressure superheated steam generator 6, it is possible to use only the heat generated in the fluidized bed combustor 7 as the heat source, but off-gases such as propane and butane obtained as gas fractions from the distillation column 5 can also be used to generate heat for atmospheric pressure superheated steam generation. For example, propane can be supplied as fuel to the burner 21 (also called the "off-gas burner" or "propane burner") located in the atmospheric pressure superheated steam generator 6, and the heat from the burner 21 can also be used to superheat the steam (for example, to heat the superheater). Off-gases generated by the thermal decomposition of waste plastics, etc., are typically obtained in the form of petroleum gas containing hydrocarbons with 1 to 4 carbon atoms, i.e., methane, ethane, propane, and butane, and are mainly obtained in the form of petroleum gas containing 3 to 4 carbon atoms, i.e., propane and butane as the main components. Here, it is also possible to supply the petroleum gas in the form of atmospheric pressure (the off-gas becomes the vacuum pump discharge pressure) to the burner 21 as fuel.

[0073] In one embodiment of the present invention, the distillation column 5 is connected to an atmospheric pressure superheated steam generator 6, particularly a burner 21 within the atmospheric pressure superheated steam generator 6, so that the propane (or off-gas containing propane, etc.) obtained therefrom can be supplied to the atmospheric pressure superheated steam generator 6. For example, the apparatus 1 includes an off-gas (petroleum gas equivalent component) supply line 14 connecting the distillation column 5 (preferably at or near the top of the column) to the atmospheric pressure superheated steam generator 6, particularly a burner 21 within the atmospheric pressure superheated steam generator 6. Through this line, the off-gas obtained as a gas fraction (for example, in the form of petroleum gas (PG)) is supplied to an off-gas burner located in the atmospheric pressure superheated steam generator 6 and used as fuel for the off-gas burner. Here, the off-gas can also be supplied to the burner 21 via a tank 38 (for example, a PG buffer tank or an off-gas tank) located in the middle of the petroleum gas (PG) supply line 14 (for example, after the off-gas has been temporarily stored in the tank). The petroleum gas (PG) supply line can be, for example, pipes, conduits, or piping, but is not particularly limited in terms of material, shape, or diameter (inner diameter, outer diameter, etc.), as long as it can properly deliver the off-gas from the distillation column 5 to the atmospheric pressure superheated steam generator 6. The separation of the decomposition gas in step d) yields low-carbon hydrocarbon gases such as propane and butane (also called "off-gases"). These off-gases can also be supplied to the atmospheric pressure superheated steam generator and used as part of the fuel for generating atmospheric pressure superheated steam.

[0074] Typically, the combustion gas temperature in a fluidized bed combustor reaches 800-1000°C, for example, 850-950°C. For example, preheated air from a recuperator is supplied to the combustor via combustion air fan control to maintain an appropriate air-fuel ratio (air surplus) of 1.2-1.5.

[0075] In one preferred embodiment of the present invention, the fluidized bed combustor 7 is configured to return at least a portion of the fluidized sand after combustion of residual combustible material in the fluidized bed combustor 7 (particularly in the fluidized bed 8) to the fluidized bed gasifier 2. That is, in this embodiment, the fluidized sand remaining after combustion of residual combustible material in the fluidized bed combustor 7 is returned to the fluidized bed gasifier 2 and recycled as fluidized sand for the fluidized bed 3 of the fluidized bed gasifier 2. For example, the apparatus 1 is equipped with a fluidized sand return line 10 that extracts at least a portion of the fluidized sand in the fluidized bed combustor 7 and returns it to the fluidized bed gasifier 2, thereby enabling the above-described return (recycling).

[0076] Preferably, the recycling of fluidized sand is achieved not by directly returning the fluidized sand to the fluidized bed gasifier 2, but by returning it to the fluidized bed gasifier 2 via a supply device 4. For example, the fluidized sand return line 10 connects the fluidized bed combustor 7 (e.g., the bottom) and the supply device 4 (e.g., the raw material inlet of the hopper 11), and the fluidized sand is sent / transported from the former to the latter. The fluidized sand return line 10 can be, for example, a pipe, conduit, piping, transport system, etc., but is not particularly limited in terms of material, shape, and size (inner diameter, outer diameter, etc.), as long as it can properly return the fluidized sand from the fluidized bed combustor 7 to the fluidized bed gasifier 2. Alternatively, the fluidized sand return line 10 may consist of a device such as a fluidized sand discharge device 15, preferably a screw conveyor. In this way, by using the supply device 4, the fluidized sand to be recycled is introduced into the fluidized bed gasifier 2 along with the supplied raw materials. The fluidized sand is not only recycled, but the layer of sand also blocks the air intrusion path into the pyrolysis furnace, contributing to maintaining the airtightness of the supplied raw materials and, consequently, maintaining non-combustion conditions inside the fluidized bed gasifier 2.

[0077] Accordingly, in one embodiment of the present invention, the apparatus 1 comprises a fluidized sand recovery line 9 that extracts at least a portion of the used fluidized sand from the fluidized bed gasifier 2 and supplies it to the fluidized bed combustor 7, and a fluidized sand return line 10 that extracts at least a portion of the fluidized sand in the fluidized bed combustor 7 and returns it to the fluidized bed gasifier 2, wherein the fluidized sand return line 10 is connected to the fluidized bed gasifier 2 via the supply device 4. For example, a constant amount of fluidized sand may be extracted from both the fluidized bed gasifier 2 and the fluidized bed combustor 7 at all times, and in this case, the amount extracted from both may be the same (or substantially the same) amount. With this configuration, the present invention achieves the circulation of (fluidized) sand between the two types of fluidized beds. As a result, residual combustible material generated in the fluidized bed gasifier 2 can be used as fuel for the fluidized bed combustor 7 of the atmospheric pressure superheated steam generator 6 in the form of used fluidized sand. Furthermore, the sand used in the fluidized bed combustor 7 can be returned to the fluidized bed gasifier 2 for recycling.

[0078] As described above, when the apparatus is in operation, fluidized beds 3 and 8 must be formed in the fluidized bed gasifier 2 and the fluidized bed combustor 7. For example, operation starts after the required amount of fluidized sand is filled into the fluidized bed gasifier 2 and the fluidized bed combustor 7. However, used fluidized sand is sent from the gasifier 2 to the fluidized bed combustor 7, so fluidized sand is supplied to the gasifier 2 to compensate for the decrease in fluidized sand in the gasifier 2. The fluidized sand can be fed into the supply device as appropriate (at an appropriate time), preferably together with the supply material as described above, more preferably mixed with the supply material before being fed into the supply device. However, more preferably, from the viewpoint of ensuring the airtightness of the supply material, sand is always added to the supply material when the supply material is supplied into the supply device. For example, when the apparatus 1 is in continuous operation, the supply material is continuously supplied to the supply device 4, and at the same time, fluidized sand (fresh fluidized sand and / or recycled fluidized sand) is also continuously supplied to the supply device 4, preferably pre-mixed with the supply material. Preferably, the amount of fluidized sand supplied to the supply device is such that it balances (typically equal to) the amount of used fluidized sand removed from the fluidized bed 3 of the fluidized bed gasifier 2 for supply to the fluidized bed combustor 7 of the atmospheric pressure superheated steam generator 6.

[0079] When used fluidized sand is supplied from the fluidized bed gasifier 2 to the fluidized bed combustor 7, it may contain components such as pulverized coal (including sludge particles), tar, ash (including salt, sulfur, sulfur compounds, unreacted calcium carbonate, etc.), and FCC catalyst. Sludge, tar, sulfur, etc. are burned in the fluidized bed combustor 7. The sulfur is burned to form sulfur oxides (SOx), but as described above, it reacts with CaCO3 in the fluidized bed 8 to form harmless solid powders such as CaSO3 and CaSO4 (gypsum). Therefore, since the fluidized sand extracted from the fluidized bed 8 of the fluidized bed combustor 7 and recycled contains FCC catalyst and other harmless useful components, it is preferable to separate these from the sand, recover or remove them as needed, and then return it to the supply device 4 (especially the hopper 11). For example, CaO (quicklime) and FCC catalyst can be separated and removed by installing a vibrating screen in the fluidized sand return line 10. Furthermore, CaCl2, CaSO3, and CaSO4 can be isolated by installing a washing device in the middle of the fluidized sand return line 10, for example downstream of the vibrating screen, and washing the fluidized sand for recycling with the washing device, typically with water. This allows CaCl2 to be isolated as a (water) solution, and CaSO3 and CaSO4 to be isolated as precipitates (CaSO4 as a hydrate precipitate). CaCl2 is harmless and can be used, for example, as a de-icing agent. Also, high concentrations of CaCl2 can cause metal corrosion, and CaSO3 can solidify at low temperatures, so from these viewpoints, it is preferable to separate them from the fluidized sand. In addition, the regeneration temperature of FCC catalysts is generally 550-660°C, and the temperature inside the fluidized bed combustor 7 is well above these temperatures. Therefore, the FCC catalyst can be recycled as is without separating it from the fluidized sand, or the FCC catalyst can be separated from the fluidized sand and recovered, for example, by known separation means.

[0080] As described above, the apparatus of the present invention is compact, and the amount of decomposition gas produced in the fluidized bed gasifier is 10 tons or less per day.

[0081] The apparatus can be operated in batch mode or continuously mode. Preferably, the apparatus is operated continuously. A single operation is preferably 100 hours or longer, for example, a "Weekly Start and Stop (WSS)" operation.

[0082] As described above, the present invention also relates to a method for producing decomposed liquid and / or gaseous hydrocarbons from feedstock including waste plastics and / or waste rubber.

[0083] The above manufacturing method involves the following steps: a) A step of introducing the supply material into a fluidized bed gasifier using sand as a fluidizing medium, b) In the fluidized bed gasifier, under non-combustion conditions, the supply material introduced in step a) is brought into contact with a fluidized bed that has been fluidized with superheated steam at atmospheric pressure to thermally decompose it and generate a decomposition gas. c) A step of generating atmospheric pressure superheated steam in an atmospheric pressure superheated steam generator having a fluidized bed combustor using sand as a fluidizing medium, and supplying this to the fluidized bed gasifier in step b) in order to fluidize the fluidized bed of the fluidized bed gasifier, d) A step of separating the decomposition gas produced in step b) in a distillation column to recover the oil, and e) A step in which at least a portion of the fluidized sand containing residual combustible material generated in the fluidized bed gasifier in step b) is supplied to the fluidized bed combustor of the atmospheric pressure superheated steam generator, and the residual combustible material is burned as at least a portion of the fuel for generating atmospheric pressure superheated steam in step c), including, and Steps a) to c) and e) described above are carried out under normal pressure.

[0084] <Step a)> In step a), the supply material is introduced into a fluidized bed gasifier 2 using sand as the fluidizing medium.

[0085] The supplied raw materials include waste plastics and / or waste rubber. Waste plastics include plastic products that have been discarded after use and plastic scraps generated during their manufacturing process, as well as other waste materials mainly composed of plastic (also referred to as "waste plastics"). Waste rubber includes discarded rubber tires (waste tires) and other rubber products (also referred to as "waste rubber"). In this invention, the plastic and rubber components contained in such supplied raw materials are used as oil-based raw materials.

[0086] The aforementioned feedstock may contain foreign matter, as long as it does not significantly affect gasification or liquefaction. Those skilled in the art will understand the types and amounts of foreign matter that are acceptable. For example, even if cellulosic waste such as paper or wood chips is mixed in, these will become dry distillation gas or char particles, which can be separated and removed, for example, in the distillation process or the fluidized sand recycling process. Of course, it is also possible to use feedstock that consists (substantially) of waste plastics and / or waste rubber. Furthermore, in a fluidized bed gasifier, because sand has a high heat capacity, even if the feedstock has a relatively high moisture content, the parts that come into contact with the sand will dry in a short time, and it will then be possible to process it as a dry material without any problems.

[0087] Waste plastics often contain polyvinyl chloride (PVC) and other materials, which contain chlorine. However, in the apparatus and method of the present invention, since atmospheric pressure superheated steam, i.e., steam, is used, water-soluble substances, such as hydrogen chloride, can be separated and removed from the gasification furnace as hydrochloric acid by contact with water. Furthermore, as described above, separation and removal from the reaction system is also possible by using a detoxifying agent. However, preferably, the amount of PVC is 15% by weight or less, more preferably 10% by weight or less, based on the total weight of the supplied raw materials.

[0088] The size and shape of the raw materials supplied are not particularly limited, as long as they can be fed into the fluidized bed gasifier 2. If necessary, the raw materials supplied may be crushed or cut using known methods before being subjected to the apparatus and method of the present invention.

[0089] The aforementioned raw material may contain both waste plastic and waste rubber simultaneously. However, the raw material preferably contains only one of either waste plastic or waste rubber. In the apparatus and method of the present invention, it is preferable that the raw material containing waste plastic and the raw material containing waste rubber are processed separately.

[0090] Furthermore, the supplied raw materials may also include a chlorine decontaminant and / or a sulfur decontaminant and / or an FCC catalyst. By including these in the supplied raw materials, harmful components such as chlorine and sulfur can be efficiently removed as described above, and gasification and oil conversion by thermal decomposition can be carried out efficiently at a relatively low temperature.

[0091] The supply material to the fluidized bed gasifier can be introduced by any means. For example, the supply material may be introduced into the fluidized bed gasifier using a supply device as described above. In one embodiment, the supply material is introduced into the fluidized bed through the side wall of the fluidized bed gasifier at an upward gradient by a screw feeder, which has a screw shaft inserted into a cylindrical casing. Here, preferably, the gradient angle of the upward gradient is 10 to 35°. As described above, by introducing the supply material using such a screw feeder, fuel can be supplied into the furnace while sealing the air passage with sand. The inside of the gasifier is filled with a gas mixture of flammable gases, waste plastic oil vapor, and atmospheric pressure superheated steam at a high temperature of up to 400°C, for example, so if a large amount of air is introduced into the gasifier from the supply passage, it can cause a fire or explosion. Therefore, a device or method for introducing the oil-converting material into the gasifier while maintaining airtightness is important for a continuous oil conversion apparatus. While this problem can be avoided with batch processing, in a preferred embodiment, the device is intended for continuous processing.

[0092] <Step b)> In step b), the feed material introduced in step a) is heated in a fluidized bed gasifier under non-combustion conditions by contacting it with a fluidized bed that has been fluidized with atmospheric pressure superheated steam. As a result, the feed material, especially the plastic and / or rubber components contained therein as oil-based materials, is thermally decomposed, and a decomposition gas is generated. This decomposition gas contains various components with various molecular weights, and is a mixture of components ranging from naphthas (volatile oils: Class 1 petroleum) to solid oil components (ultra-heavy oils: Class 4 petroleum). The basic operation of the fluidized bed gasifier can be carried out in the same way as that of a gasifier of the same type. For example, in step b), the blowing velocity / flow rate of atmospheric pressure superheated steam can be set to 2 m / sec or less, for example, 0.05 m / sec to 1.5 m / sec, or 0.1 to 1 m / sec, in order to fluidize the fluidized bed.

[0093] Furthermore, the aforementioned pyrolysis can be carried out at a furnace temperature of 250 to 700°C, preferably 300 to 600°C, and more preferably 430 to 550°C (preferably the gas temperature of the free board section). For example, the pyrolysis can be carried out at a furnace temperature of 250 to 400°C. If the temperature inside the pyrolysis gasification furnace is too low, the efficiency of decomposing and gasifying / oiling plastics and rubber polymers and high-molecular structures to have 40 or fewer carbon atoms decreases. On the other hand, if the furnace temperature is too high, a phenomenon called coking occurs, in which hydrogen in hydrocarbons is released, generating black carbon particles, which can adversely affect the quality of the resulting oil. By performing pyrolysis at the furnace temperatures described above, plastic and rubber components as raw materials for oil conversion can be successfully decomposed. In particular, as described above, by introducing an FCC catalyst, it is possible to set a low furnace temperature while maintaining a high reaction rate.

[0094] <Step c)> In step c), atmospheric pressure superheated steam is generated in an atmospheric pressure superheated steam generator having a fluidized bed combustor using sand as a fluidizing medium, and this is supplied to the fluidized bed gasifier in step b) in order to fluidize the fluidized bed of the fluidized bed gasifier.

[0095] As described above, in an atmospheric pressure superheated steam generator, water is heated and boiled at atmospheric pressure to generate saturated steam at atmospheric pressure (approximately 100°C), and this saturated steam is then superheated to produce atmospheric pressure superheated steam. The temperature of the atmospheric pressure superheated steam can be set so that when the atmospheric pressure superheated steam is introduced into a fluidized bed gasifier, the furnace temperature becomes, for example, the temperature described above. For this purpose, for example, an atmospheric pressure superheated steam generator can produce atmospheric pressure superheated steam having a temperature of 400 to 650°C, more preferably 450 to 600°C, for example, 500 to 580°C or 530 to 570°C. Such atmospheric pressure superheated steam can be supplied as a fluidizing gas into a fluidized bed gasifier, for example, so that the blowing velocity / flow rate of the atmospheric pressure superheated steam is 2 m / sec or less (for example, 0.05 m / sec to 1.5 m / sec, or 0.1 to 1 m / sec), so as to cause the fluidized bed to flow.

[0096] <Step d)> In step d), the decomposition gas generated in step b) is separated in a distillation column to recover the oil. For example, the decomposition gas can be introduced into the bottom of a multi-stage distillation column, where the atmosphere changes from atmospheric pressure to a reduced pressure, and the distilled oil can be recovered by separating it into several types according to the type of oil.

[0097] As described above, the decomposition gas consists of a multi-component system containing a wide variety of components and is not separated by specific oil type. The proportion of each component follows an approximately normal distribution (Gaussian distribution) when the mass number of molecules or the number of carbon atoms in the molecule is plotted on the horizontal axis. Therefore, in step d), the decomposition gas is fed into a distillation column, where the distillation operation allows for the separation and recovery of the desired fractions as decomposed liquid hydrocarbons and / or gaseous hydrocarbons, particularly the former as oil (oil that is liquid at room temperature and pressure) and the latter as gas (gas that is gas at room temperature and pressure). The method (means, procedures, etc.) for separating each fraction from the decomposition gas using a distillation column and recovering them as needed is known to those skilled in the art, and such known techniques can also be used in the present invention.

[0098] This step, namely the separation of the decomposition gas and its recovery as each fraction (gas, oil), can be carried out under atmospheric pressure and / or reduced pressure. Specifically, for example, the separation of the decomposition gas can be carried out under atmospheric pressure or reduced pressure, and the recovery of each fraction can be carried out under atmospheric pressure. In one embodiment of the present invention, the above step can also be carried out by fractional distillation of oil using a multistage distillation column, more preferably a multistage vacuum distillation column. These distillation columns themselves, and the methods for separating and recovering various fractions as liquid and / or gaseous hydrocarbons from gaseous components containing various components using these distillation columns, are known to those skilled in the art.

[0099] In one embodiment of the present invention, the decomposition gas produced in step b) may be heated and / or brought into contact with a catalyst before being subjected to separation in the distillation column in step d). In addition, in the present invention, the residual oil (heavy residual oil) produced in the distillation column in step d) may be heated and / or brought into contact with a catalyst to obtain residual oil decomposition products, and at least a portion of these products may be returned to the distillation column. Specifically, for example, the residual oil (heavy residual oil) that does not become a fraction in the distillation column in step d) and remains at the bottom may be heated and / or brought into contact with a catalyst to decompose the residual oil polymer, obtaining lower molecular weight products. Due to the characteristic that the boiling point of these products is lower than that of the residual oil polymer, at least a portion of these products may rise and pass through the trays of the distillation column to become a fraction.

[0100] These heating and contacts with catalysts can be carried out by supplying the decomposition gas to the distillation column via the oil bath 55 described above, or by supplying the decomposition gas to a distillation column equipped with the oil bath 55 at the bottom of the column.

[0101] As described above, the decomposition gas sent to the distillation column usually contains wax components that have not been sufficiently decomposed by heat, and these accumulate at the bottom of the distillation column as high-temperature residual oil. In the above embodiment, however, such residual oil is stored in an oil bath attached to the bottom of the distillation column, for example, and heated there by a heater, such as a burner, installed in the oil bath. This heating yields pyrolysis products (residual oil pyrolysis products), and the components contained in these products have lower molecular weights and boiling points than those in the residual oil. Therefore, at least some of these components can rise from the oil bath back to the distillation column, preferably to the trays of the distillation column. In other words, at least some of the residual oil pyrolysis products (components whose molecular weights and boiling points have decreased to the extent that they can rise from the oil bath back to the distillation column) are returned from the oil bath to the distillation column, preferably to the trays of the distillation column, and ultimately these components can also rise up the trays of the distillation column and become fractions. In order to properly promote the decomposition of the heavy residue oil, the heavy residue oil is heated to, for example, 400 to 1500°C, preferably 500 to 1000°C, and more preferably 700 to 900°C by the aforementioned heating process.

[0102] Furthermore, by including a catalyst, preferably an FCC catalyst, in the oil bath 55, for example, decomposition can be promoted by contact with the catalyst. In this case as well, decomposition products (residual oil catalyst decomposition products) are obtained by the action of the catalyst, and since the molecular weight and boiling point of the components contained in these products are lower than those in the residual oil, at least some of these components can rise and return from the oil bath to the distillation column, preferably to the trays of the distillation column. In addition, the decomposition gas generated in step b) can be heated in the oil bath 55 and / or brought into contact with a catalyst before being subjected to separation in the distillation column in step d).

[0103] The aforementioned heating and contact with the catalyst are carried out under atmospheric pressure or reduced pressure, preferably under reduced pressure. The decomposition gas produced in step b) may contain wax components and the like that are carried along by the atmospheric pressure superheated steam, but it has been found that including such a treatment can reduce the amount of such components and homogenize the recovered oil product. As for the FCC catalyst used in the oil bath 55, the one described above for thermal decomposition in the fluidized bed gasifier 2 can be used.

[0104] <Step e)> In step e), at least a portion of the fluidized sand containing residual combustible material generated in the fluidized bed gasifier is supplied to the fluidized bed combustor of the atmospheric pressure superheated steam generator, and the residual combustible material is burned as at least a portion of the fuel for generating atmospheric pressure superheated steam in step c). In step b), the feed material is thermally decomposed to produce decomposition gas, but organic matter and other materials (residual combustible material) that remain in the gasifier without being completely gasified from the feed material exist. Such residual combustible material mainly exists together with the fluidized sand (for example, adhering to the surface of the fluidized sand). On the other hand, the atmospheric pressure superheated steam generator is equipped with a fluidized bed combustor that uses sand as a fluidizing medium, and the heat generated by burning fuel in the fluidized bed combustor is used as at least a portion of the heat source for generating atmospheric pressure superheated steam. In step e), the residual combustible material is supplied to the fluidized bed combustor and burned as at least a portion of the fuel. This allows residual combustible material to be reused as energy for generating superheated steam at atmospheric pressure, thereby improving the efficiency and reducing the cost of the method. Preferably, the primary combustion furnace floor area of ​​the fluidized bed combustor is 0.5 square meters or less and conforms to the "Structural Standards for Small Incinerators" set forth by the Ministry of the Environment.

[0105] Furthermore, as described above, propane obtained during the separation of the decomposition gas in step d) can also be used as fuel for the atmospheric pressure superheated steam generator. Accordingly, in one embodiment of the present invention, the propane (typically in the form of petroleum gas including butane, preferably petroleum gas mainly composed of propane) is supplied to the atmospheric pressure superheated steam generator and this propane is also used as part of the fuel for the fluidized bed combustor. This further promotes the efficiency and cost reduction of the method.

[0106] Here, steps a) to c) and e) can be carried out under atmospheric pressure, and step d) can be carried out under atmospheric pressure or reduced pressure. In one embodiment of the present invention, the method is carried out under reduced pressure only for the operation / conductance in the distillation column (and optionally the oil bath), while the other steps / operations / conductances are carried out under atmospheric pressure. Thus, the present invention can achieve high safety because all or most of the steps can be carried out under atmospheric pressure.

[0107] In one preferred embodiment, the method further includes step f): f) A step of returning the fluidized sand generated after burning the residual combustible material in step e) to the fluidized bed gasification furnace.

[0108] In step e) above, the fluidized sand from the fluidized bed gasifier contains residual combustible material, so it is supplied to the fluidized bed combustor of the atmospheric pressure superheated steam generator and burned as fuel. In step f), however, the fluidized sand remaining after combustion is returned to the fluidized bed gasifier. This allows for the recycling of the fluidized sand, thereby improving the efficiency and reducing the cost of the method. In one preferred embodiment of the present invention, the fluidized sand is returned to the fluidized bed gasifier after being separated from ash and salt.

[0109] The manufacturing method of the present invention is particularly suitable for pyrolysis / oil conversion using a small-scale apparatus, for example, such a small-scale apparatus has a production rate of 10 tons or less per day (from step b) of the decomposition gas.

[0110] Furthermore, the above method may be carried out in a batch or continuous manner, but it is preferably carried out in a continuous manner. When operated in a continuous manner, the circulation (recycling) of fluidized sand between the two types of fluidized beds and the supply of atmospheric pressure superheated steam from the atmospheric pressure superheated steam generator to the gasifier function in a more interconnected manner, further promoting the efficiency and cost reduction of the above method.

[0111] In the method described above, the order in which steps a) to e) and optionally f) are performed is not particularly limited, regardless of whether they are performed in batch or sequential order. Of course, it is also possible to perform several steps simultaneously as appropriate. As long as the method is performed in such a way that it includes all of steps a) to e) and optionally f), it will be understood by those skilled in the art that each step can be performed in any order and timing depending on the situation.

[0112] By this method, the decomposed liquid and / or gaseous hydrocarbons can be produced as gas fractions such as propane (typically in the form of petroleum gas, including butane), naphtha fractions, kerosene fractions, light oil fractions, heavy oil fractions, and so on.

[0113] By using the method and apparatus of the present invention as described above, waste plastics and / or waste rubbers can be converted into oil with high efficiency while ensuring high safety. Furthermore, in the present invention, residual combustible material from the gasification furnace is sent together with fluidized sand to the fluidized bed combustor of an atmospheric pressure superheated steam generator and used as fuel for combustion in the combustor. This provides the heat necessary for generating atmospheric pressure superheated steam, thus achieving energy savings and cost reduction. In addition, the method and apparatus of the present invention are particularly well-suited to miniaturization. For example, when using the method and apparatus of the present invention, chlorine content that may be contained in waste plastics, sulfur content derived from waste tires, etc., can be separated and removed from the reaction system with simple operation without the need to separately install independent dechlorination or desulfurization equipment. Moreover, in the apparatus and method of the present invention, pre-mixed raw materials can be fed into a single hopper. Therefore, there is no need to install multiple hoppers assigned to each raw material or abrasive, which also greatly contributes to the ease of implementation of the apparatus and method, as well as to miniaturization of the apparatus. These issues, which cannot be achieved simply by scaling down and miniaturizing the configuration of related, known large-scale equipment, can be achieved with the apparatus and method of the present invention, which uses two types of fluidized beds while circulating fluidized sand, as described above. [Brief explanation of the drawing]

[0114] [Figure 1] Figure 1 is a scheme diagram showing one embodiment of the pyrolysis gasification / oil conversion apparatus and method of the present invention. [Figure 2] Figure 2 is a schematic diagram showing one embodiment of the configuration of the pyrolysis gasification / oil conversion apparatus of the present invention. [Figure 3] Figure 3 is a schematic diagram showing one embodiment of the configuration of the pyrolysis gasification / oil conversion apparatus of the present invention. [Explanation of Symbols]

[0115] 1. Pyrolysis gasification / oil conversion equipment 2. Fluidized bed gasifier 3. Fluidized bed 4. Supply Devices 5. Distillation column 6. Atmospheric pressure superheated steam generator 7. Fluidized bed combustion chamber 8. Fluidized bed 9. Fluidized sand recovery line 10. Flowable sand return line 11 Hopper 12 Screw feeders 13. Decomposition gas supply line 14. Oil and Gas (PG) Supply Lines 15. Fluidized Sand Discharge Device 16 Evaporator 17 Superheater 18. Atmospheric pressure superheated steam supply line 19 Water purifier 20 Steam supply lines 21 Burner 22 Distillation Tank: Naphtha (30 kg / h) 23 Distillation Tank: Kerosene, equivalent to JP (40 kg / h) 24 Distillation Tanks: Equivalent to diesel fuel (50 kg / h) 25 Distillation Tank: Equivalent to heavy oil (30 kg / h) 26. Distillate Condenser 27. Distillation pump 28 Check valve 29 Vibrating sieve 30 Cleaning devices 31 Air diffuser 32 Air diffuser 33 Air preheater 34. Water-sealed vacuum pump (simultaneous drain recovery) 35 Neutralization Tank 36 Radiator 37. Combustion device (off-gas (PG) + waste oil mixed combustion burner) 38 PG Buffer Tank 39 Gas-liquid separation 40 Combustion air 41 Preheated air (400℃) 42. Superheated steam at atmospheric pressure (approximately 550°C, 420 kg / h, atmospheric pressure) 43 liquid 44 Combustion exhaust gas 45 Sand 46. ​​Residual heavy oil (solid oil at room temperature (tar, wax, etc.)) (18 kg / h) 47. Fluidized sand + FCC catalyst + pulverized coal (sludge) + tar + ash (approx. 180 kg / h) 48. Other fuels for heat sources (however, the sand must be returned) (approximately 240 kg / h) 49 Fluidized sand (silica sand) + FCC catalyst particles 50 Sand return 51 CaCl2 solution; CaSO3 precipitate; CaSO4 precipitate (hydrate) 52 CaO (quicklime) 53. Waste plastic and waste rubber raw materials (input: 400 kg / h) (PVC can be mixed in (10% or less by weight)) 54. Calcium carbonate (from oyster shells, etc.) 55 Oil Bath 56. Mix with fluidized sand (silica sand, etc.), FCC catalyst (granules / powder), and calcium carbonate (decontaminant) (total approx. 600 kg / h) 57. Gasification (180 kg / h) 58. Oil Sand (Tar Sand) Condition 59 Raw materials: Plastics and elastomers 60. Fluidized sand (and mixtures thereof) 61. Pyrolysis vapor (oil vapor and PG components) 62 Superheated steam at atmospheric pressure and water 63 Distilled waste plastic oil 64. Undistilled heavy residue oil 65 Combustion air 66 Combustion exhaust gas 67 Water / Neutralizing Solution 68 Freeboard Section

Claims

1. A method for producing decomposed liquid and / or gaseous hydrocarbons from a supply of raw materials including waste plastics and / or waste rubber, a) A step of introducing the supply material into a fluidized bed gasifier using sand as a fluid medium, b) In the fluidized bed gasifier, under non-combustion conditions, the supply material introduced in step a) is brought into contact with a fluidized bed that has been fluidized with atmospheric pressure superheated steam to thermally decompose it and generate a decomposition gas. c) A step of generating atmospheric pressure superheated steam in an atmospheric pressure superheated steam generator having a fluidized bed combustor using sand as a fluidizing medium, and supplying this to the fluidized bed gasifier in step b) in order to fluidize the fluidized bed of the fluidized bed gasifier, d) A step of separating the decomposition gas produced in step b) in a distillation column to recover the oil, and e) A step in which at least a portion of the fluidized sand containing residual combustible material generated in the fluidized bed gasifier in step b) is supplied to the fluidized bed combustor of the atmospheric pressure superheated steam generator, and the residual combustible material is burned as at least a portion of the fuel for generating atmospheric pressure superheated steam in step c), including, and The method wherein steps a) to c) and e) are performed under normal pressure.

2. The following steps: f) A step of returning the fluidized sand generated after burning the residual combustible material in step e) to the fluidized bed gasifier, The method according to claim 1, further comprising:

3. The method according to claim 2, wherein in step f), the fluidized sand is added to the supply material introduced in step a) and returned to the fluidized bed gasifier.

4. The method according to claim 1 or 2, wherein the supply raw material introduced in step a) further comprises a chlorine decontaminant and / or a sulfur decontaminant and / or an FCC catalyst.

5. The method according to claim 1 or 2, wherein in step a), the supply material is introduced into the fluidized bed at an upward gradient through the side wall of the fluidized bed gasifier by a screw feeder having a screw shaft inserted into a cylindrical casing.

6. The method according to claim 5, wherein the gradient angle of the upward slope is 10 to 35°.

7. The method according to claim 1 or 2, wherein the separation of the decomposition gas in step d) is performed using a multi-stage vacuum distillation column.

8. The method according to claim 1 or 2, wherein in step d), the residual oil produced in the distillation column is heated, and at least a portion of the residual oil thermal decomposition product obtained thereby is returned to the distillation column.

9. The method according to claim 1 or 2, wherein propane is obtained by the separation of the decomposition gas in step d), and the propane is also supplied to the atmospheric pressure superheated steam generator and used as part of the fuel for generating atmospheric pressure superheated steam.

10. The method according to claim 1 or 2, wherein in step b), the blowing velocity of the atmospheric pressure superheated steam used to fluidize the fluidized bed is 1 m / second or less.

11. The method according to claim 1 or 2, wherein step b) is performed at a furnace temperature of 250 to 400°C.

12. The method according to claim 1 or 2, wherein the amount of decomposition gas generated from step b) is 10 tons or less per day.

13. The method according to claim 1 or 2, which is carried out in a continuous manner.

14. A pyrolysis gasification / oil conversion apparatus for producing decomposed liquid and / or gaseous hydrocarbons from feedstock including waste plastics and / or waste rubber, - A fluidized bed gasifier adapted to include a fluidized bed with sand as the fluidizing medium, which is fluidized by atmospheric pressure superheated steam at atmospheric pressure and brought into contact with the supply material under non-combustion conditions to generate decomposition gas. - A supply device that supplies the raw material to the fluidized bed gasifier at atmospheric pressure. - A distillation column to which the decomposition gas produced in the fluidized bed gasifier is sent, and to which the decomposition gas is separated under atmospheric or reduced pressure to recover oil, and - An atmospheric pressure superheated steam generator that supplies atmospheric pressure superheated steam to the fluidized bed gasifier at atmospheric pressure. Includes, The atmospheric pressure superheated steam generator is a fluidized bed combustor that burns fuel for generating atmospheric pressure superheated steam, and includes a fluidized bed combustor to which at least a portion of the spent fluidized sand produced in the fluidized bed gasifier is sent. The aforementioned device.

15. The apparatus according to claim 14, wherein the fluidized bed combustor is configured to return at least a portion of the fluidized sand in the fluidized bed combustor to the fluidized bed gasifier.

16. The apparatus according to claim 15, comprising: a fluidized sand recovery line for withdrawing at least a portion of the used fluidized sand from the fluidized bed gasifier and supplying it to the fluidized bed combustor; and a fluidized sand return line for withdrawing at least a portion of the fluidized sand from the fluidized bed combustor and returning it to the fluidized bed gasifier, wherein the fluidized sand return line is connected to the fluidized bed gasifier via the supply device.

17. The apparatus according to claim 14 or 15, wherein the supply device is a screw feeder in which a screw shaft is inserted into a cylindrical casing, and the screw feeder is connected to the fluidized bed gasifier at an upward slope.

18. The apparatus according to claim 17, wherein the gradient angle of the aforementioned upward slope is 10 to 35°.

19. The apparatus according to claim 17, wherein the supply device further comprises a hopper adapted to allow the screw feeder to jointly introduce the supply material, the fluidized sand for the fluidized bed gasifier, and optionally chlorine and / or sulfur decontaminants and / or optionally FCC catalyst.

20. The apparatus according to claim 14 or 15, wherein the distillation column is connected to the atmospheric pressure superheated steam generator so that the propane obtained therefrom can be supplied to the atmospheric pressure superheated steam generator.

21. The apparatus according to claim 14 or 15, further comprising an oil bath having a heater between the fluidized bed gasifier and the distillation column, or at the bottom of the distillation column.

22. The apparatus according to claim 14 or 15, wherein the amount of decomposition gas produced in the fluidized bed gasifier is 10 tons or less per day.

23. The apparatus according to claim 14 or 15, which is a continuous-type apparatus.

24. The apparatus according to claim 14 or 15, wherein the fluidized bed combustor is provided with an air inlet.

25. The apparatus according to claim 14 or 15 for carrying out the method according to claim 1.

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